The present invention relates to a pressure vessel (1, 1′), having a lower part (20) and the lid (24) which can be locked to one another, in order, in the state in which they are locked to one another, to surround a reaction chamber (22) on all sides as a pressure space for initiating and/or promoting chemical and/or physical pressure reactions of samples (P) which are received in the reaction chamber (22), and a fluid inlet (FE) with a check valve (4) for feeding a fluid into the reaction chamber (22), the check valve (4) extending at least partially in the lid (24).

A carbonylation process for producing acetic acid including: (a) carbonylating methanol or its reactive derivatives in the presence of a Group VIII metal catalyst and methyl iodide promoter to produce a liquid reaction mixture including acetic acid, water, methyl acetate and methyl iodide; (b) feeding the liquid reaction mixture to a flash vessel; (c) flashing the reaction mixture to produce a crude product vapor stream.

Methods of controlling olefin polymerization reactor systems may include a) selecting n input variables, each input variable corresponding to a process condition for an olefin polymerization process; b) identifying m response variables corresponding to a measurable polymer property; c) adjusting one of more of the n input variables using the olefin polymerization reactor system and measuring each of the m response variables as a function of the input variables for olefin polymers; d) analyzing the change in each of the response variables as a function of the input variables to determine coefficients; e) calculating a Response Surface Model (RSM) for each response variable determined in step d); f) applying n selected input variables to the calculated RSM to predict one or more of m target response variables; and g) using the n selected input variables to operate the olefin polymerization reactor system and provide a polyolefin product.

A continuous process for the manufacture of a polyamide, the process comprising the steps of: (i) flowing a stream A comprising a moltendicarboxylic acid, or a molten dicarboxylic acid-rich mixture comprising a dicarboxylic acid and a diamine, through a first stage and at least one more reaction stage of a vertical multistage reactor, wherein the first stage is at the top of the reactor; (ii) counter-currently flowing a stream B comprising a diamine as either a vapor or a diamine-rich liquid through at least one of the stages below the first reaction stage of said vertical multistage reactor; (iii) accumulating a liquid phase material P comprising polyamide at and/or below the final stage of said reactor; wherein said reactor is equipped with internal features suitable for effecting contact between counter-currently flowing streams A and B; and wherein the process further comprises controlling the viscosity of said liquid phase material P by directly controlling the chemical equilibrium of the polyamidation reaction or by controlling stream B so that the amounts of diamine and dicarboxylic acid introduced into the reactor during the process are stoichiometrically imbalanced. The invention further provides a vertical multistage reactor configured to implement said process.

Techniques regarding the synthesis of one or more polymers of a target polymer class are provided. For example, one or more embodiments described herein can comprise a system, which can comprise a memory that can store computer executable components. The system can also comprise a processor, operably coupled to the memory, and that can execute the computer executable components stored in the memory. The computer executable components can comprise a recommendation component that can generate a recommended chemical reactor control setting for inverse synthesis of a polymer based on a target polymer characteristic and reactor training data.

A method for determining temperature information for a plurality of tubes in a furnace where one or more digital images provide temperature information for imaged tubes, and temperature information for non-imaged tubes is determined from the temperature information for the imaged tubes and measured temperatures of combined effluent from the imaged and non-imaged tubes.

A system for reducing dioxygen (O.sub.2) present in vapors from oil storage tanks. The system may include an inlet that receives vapors from the tanks; a heating device coupled with the inlet that heats vapors to a first temperature to form heated vapor; and a vessel coupled receiving heated vapor and containing at least one catalyst to reduce dioxygen from the heated vapor. The catalyst may include palladium, and the vessel may include zinc oxide to remove sulfur from the heated vapor. A compressor may be used to compress the vapors. A controller may be provided to monitor O.sub.2 concentration in heated vapor, and the controller directs flow of heated vapor to a gas pipeline if the O.sub.2 concentration is below a predetermined level; or if the O.sub.2 concentration is unacceptably high, the controller directs flow of vapor to be re-circulated within the system to further reduce O.sub.2 concentration therein.

The invention relates to a system for generating superheated steam using hydrogen peroxide, formed by: a container for storing hydrogen peroxide, which stores a solution of peroxide that is used during the reaction to generate superheated steam; a hydrogen peroxide discharge pump connected to a first connecting duct, said discharge pump being used to pump the hydrogen peroxide solution to a reaction container via a second connecting duct; and a steam generating reaction container or reactor, in which the reaction takes place and the superheated steam is generated, said reaction container or reactor receiving the hydrogen peroxide solution in order for the reaction to take place and the superheated steam to be generated and subsequently conveyed through a nozzle and an outlet duct towards installations that are to undergo cleaning and/or stimulation.

In the hydroconversion processes of heavy hydrocarbon oils, in which the hydrogen is introduced at the reactor base by bubbling, the low diffusion rate of hydrogen, from the gas phase to the reaction liquid, limits the degree of conversion. The process circumvents the obstacle of the limited amount of reactant hydrogen by using a slurry bubble column reactor which reduces the formation of light hydrocarbon products, and therefore the hydrogen required for the hydroconversion, allowing to operate at full conversion.

Methods of controlling olefin polymerization reactor systems are provided herein. In some aspects, the methods include a) selecting n input variables, each input variable corresponding to a process condition for an olefin polymerization process; b) identifying m response variables, each response variable corresponding to a measurable polymer property; c) adjusting one of more of the n input variables in a plurality of polymerization reactions using the olefin polymerization reactor system, to provide a plurality of olefin polymers and measuring each of the m response variables as a function of the input variables for each olefin polymer; d) analyzing the change in each of the response variables as a function of the input variables to determine the coefficients; e) calculating a Response Surface Model (RSM) using general equations for each response variable determined in step d) to correlate any combination of the n input variables with one or more of m response variables; f) applying n selected input variables to the calculated Response Surface Model (RSM) to predict one or more of m target response variables, each target response variable corresponding to a measurable polymer property; and g) using the n selected input variables I.sup.s1 to I.sup.sn to operate the olefin polymerization reactor system and provide a polyolefin product.